US9468908B2 - Reduction catalysts - Google Patents

Reduction catalysts Download PDF

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US9468908B2
US9468908B2 US13/894,351 US201313894351A US9468908B2 US 9468908 B2 US9468908 B2 US 9468908B2 US 201313894351 A US201313894351 A US 201313894351A US 9468908 B2 US9468908 B2 US 9468908B2
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catalyst
range
support
platinum
rhodium
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US20130310605A1 (en
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George Fredrick Salem
Guang Zhu
Alfred Gerhard Hagemeyer
Eric L. Dias
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Archer Daniels Midland Co
Renovia Inc
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Renovia Inc
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46—Ruthenium, rhodium, osmium or iridium
    • B01J23/464—Rhodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063—Titanium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/066—Zirconium or hafnium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J35/1014—
    • B01J35/1061—
    • B01J35/1066—
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/613—10-100 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64—Pore diameter
    • B01J35/647—2-50 nm
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64—Pore diameter
    • B01J35/651—50-500 nm
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • B01J37/0205—Impregnation in several steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/024—Multiple impregnation or coating
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/347—Preparation of carboxylic acids or their salts, halides or anhydrides by reactions not involving formation of carboxyl groups
    • C07C51/377—Preparation of carboxylic acids or their salts, halides or anhydrides by reactions not involving formation of carboxyl groups by splitting-off hydrogen or functional groups; by hydrogenolysis of functional groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C55/00—Saturated compounds having more than one carboxyl group bound to acyclic carbon atoms
    • C07C55/02—Dicarboxylic acids
    • C07C55/14—Adipic acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/18—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/58—Platinum group metals with alkali- or alkaline earth metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites

Definitions

  • the present invention relates generally to heterogeneous catalysts comprised of platinum and rhodium on a support at least the outer surfaces of which are selected from the group consisting of zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites and mixtures thereof.
  • the catalysts of the present invention are particularly useful for the selective reduction of compositions of the general formula ROOC(CX) y COOR, where “y” is at least 2, “X” is, independently, selected from the group of hydroxyl, oxo, halo, acyloxy and hydrogen provided that at least one X is not hydrogen, and each “R” is, independently, selected from the group of salt-forming ions, hydrogen and hydrocarbyl or substituted hydrocarbyl or a mono- or di-lactone thereof, to dicarboxylic acids and derivatives thereof. More particularly, the present invention is directed to catalysts for the selective hydrodeoxygenation of such compositions to dicarboxylic acids and/or derivatives thereof, especially adipic acid and/or derivatives thereof.
  • Crude oil is currently the source of most commodity and specialty organic chemicals. Many of these chemicals are employed in the manufacture of polymers and other materials. Examples include ethylene, propylene, styrene, bisphenol A, terephthalic acid, adipic acid, caprolactam, hexamethylene diamine, adiponitrile, caprolactone, acrylic acid, acrylonitrile, 1,6-hexanediol, 1,3-propanediol, and others. Crude oil is first refined into hydrocarbon intermediates such as ethylene, propylene, benzene, and cyclohexane. These hydrocarbon intermediates are then typically selectively oxidized using various processes to produce the desired chemical.
  • hydrocarbon intermediates such as ethylene, propylene, benzene, and cyclohexane.
  • crude oil is refined into cyclohexane which is then selectively oxidized to “KA oil” which is then further oxidized for the production of adipic acid, an important industrial monomer used for the production of nylon 6,6.
  • KA oil an important industrial monomer used for the production of nylon 6,6.
  • Many known processes are employed industrially to produce these petrochemicals from precursors found in crude oil. For example, see Ullmann's Encyclopedia of Industrial Chemistry , Wiley 2009 (7th edition), which is incorporated herein by reference.
  • the present invention is directed to catalyst compositions comprising platinum and rhodium and a support at least the exposed surfaces of which are selected from the group of zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites and mixtures thereof, wherein the molar ratio of platinum to rhodium on the support is in the range of from about 3:1 to about 1:2 and the total weight percent of platinum and rhodium is less than about 10 wt %.
  • at least a portion of the platinum and rhodium are impregnated into the support so as to form a metal-impregnated outer shell surrounding a core of essentially un-impregnated support material.
  • the molar ratio of platinum to rhodium is in the range of about 3:1 to about 1:1.
  • the average pore diameter of the support is in the range of from about 5 nm to about 70 nm. In some embodiments, the average pore diameter of the support is in the range of from about 5 nm to about 40 nm.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 200 m 2 /g. In some embodiments, the surface area of the support is in the range of between about 15 m 2 /g and about 125 m 2 /g.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 60 m 2 /g.
  • at least a portion of the platinum is present as Pt(0).
  • at least a portion of the rhodium is present as Rh(0).
  • the particle sizes of the metals are in the range of from about 2 nm to about 30 nm.
  • the particle sizes of the metals are in the range of from about 2 nm to about 20 nm.
  • the particle sizes of the metals are in the range of from about 2 nm to about 12 nm.
  • platinum is present in an amount up to about 1.4 wt %.
  • rhodium is present in an amount up to about 0.8 wt %. In some embodiments, the total amount of platinum and rhodium present is equal to or less than about 4 wt %; in other embodiments, the total amount is equal to or less than about 2 wt %. In some embodiments, the total amount of platinum and rhodium present is in the range of from about 0.2 wt % to about 1.5 wt %. In some embodiments, the catalyst further comprises a metal selected from the group of palladium, molybdenum and tungsten. In some embodiments, the catalyst is a shell type catalyst the outer surfaces of which are impregnated with the metals so as to create a metal-impregnated outer shell having a thickness equal to or less than about 150 ⁇ m.
  • the present invention is also directed to heterogeneous catalyst compositions useful for the selective hydrodeoxygenation of compositions of the general formula ROOC(CX) y COOR, where “y” is at least 2, “X” is, independently, selected from the group of hydroxyl, oxo, halo, acyloxy and hydrogen provided that at least one X is not hydrogen, and each “R” is, independently, selected from the group of salt-forming ions, hydrogen and hydrocarbyl or substituted hydrocarbyl or a mono- or di-lactone thereof, to dicarboxylic acids and derivatives thereof wherein the catalyst comprises platinum and rhodium and a support selected from the group of zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites and mixtures thereof, the molar ratio of platinum to rhodium on the support is in the range of from about 3:1 to about 1:2 and the total weight percent of platinum and rhodium is less than about 4 wt % (of the total
  • the platinum and rhodium are impregnated into the support so as to form a metal-impregnated outer shell surrounding a core of essentially un-impregnated support material.
  • the molar ratio of platinum to rhodium is in the range of about 3:1 to about 1:1.
  • the average pore diameter of the support is in the range of from about 5 nm to about 70 nm. In some embodiments, the average pore diameter of the support is in the range of from about 5 nm to about 40 nm.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 200 m 2 /g.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 125 m 2 /g. In some embodiments, the surface area of the support is in the range of between about 15 m 2 /g and about 60 m 2 /g. In some embodiments, at least a portion of the platinum is present as Pt(0). In some embodiments, at least a portion of the rhodium is present as Rh(0). In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 30 nm. In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 20 nm.
  • the particle sizes of the metals are in the range of from about 2 nm to about 12 nm.
  • platinum is present in an amount up to about 1.4 wt %.
  • rhodium is present in an amount up to about 0.8 wt %.
  • the total amount of platinum and rhodium present is in the range of from about 0.2 wt % to about 1.5 wt %.
  • the catalyst further comprises a metal selected from the group of palladium, molybdenum and tungsten.
  • the catalyst is a shell type catalyst the outer surfaces of which are impregnated with the metals so as to create a metal-impregnated outer shell having a thickness equal to or less than about 150 ⁇ m.
  • the present invention is further directed to selective hydrodeoxygenation catalysts comprising platinum and rhodium and a support at least the exposed surfaces of which are selected from the group of zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites, and mixtures thereof, wherein the molar ratio of platinum to rhodium on the support is in the range of from about 3:1 to about 1:2, the total weight percent of platinum and rhodium is less than about 10 wt %, and the average pore diameter of the catalyst is in the range of from about 5 nm to about 70 nm.
  • the platinum and rhodium are impregnated into the support so as to form a metal-impregnated outer shell surrounding a core of essentially un-impregnated support material.
  • the molar ratio of platinum to rhodium is in the range of about 3:1 to about 1:1.
  • the average pore diameter of the support is in the range of from about 5 nm to about 40 nm.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 200 m 2 /g. In some embodiments, the surface area of the support is in the range of between about 15 m 2 /g and about 125 m 2 /g.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 60 m 2 /g.
  • at least a portion of the platinum is present as Pt(0).
  • at least a portion of the rhodium is present as Rh(0).
  • the particle sizes of the metals are in the range of from about 2 nm to about 30 nm.
  • the particle sizes of the metals are in the range of from about 2 nm to about 20 nm.
  • the particle sizes of the metals are in the range of from about 2 nm to about 12 nm.
  • platinum is present in an amount up to about 1.4 wt %.
  • rhodium is present in an amount up to about 0.8 wt %. In some embodiments, the total amount of platinum and rhodium present is equal to or less than about 4 wt %; in other embodiments, the total amount is equal to or less than about 2 wt %. In some embodiments, the total amount of platinum and rhodium present is in the range of from about 0.2 wt % to about 1.5 wt %. In some embodiments, the catalyst further comprises a metal selected from the group of palladium, molybdenum and tungsten. In some embodiments, the catalyst is a shell type catalyst the outer surfaces of which are impregnated with the metals so as to create a metal-impregnated outer shell having a thickness equal to or less than about 150 ⁇ m.
  • the present invention is directed to catalysts comprising platinum and rhodium and a support at least the outer surfaces of which are selected from the group consisting of zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites and mixtures thereof, wherein the molar ratio of platinum to rhodium on the support is in the range of from about 3:1 to about 1:2, the total weight percent of platinum and rhodium is in the range of about 0.2 wt % to about 4 wt %, and the surface area of the catalyst is equal to or less than about 60 m 2 /g.
  • the platinum and rhodium are impregnated into the support so as to form a metal-impregnated outer shell surrounding a core of essentially un-impregnated support material.
  • the molar ratio of platinum to rhodium is in the range of about 3:1 to about 1:1.
  • the average pore diameter of the support is in the range of from about 5 nm to about 70 nm. In some embodiments, the average pore diameter of the support is in the range of from about 5 nm to about 40 nm.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 60 m 2 /g.
  • the platinum is present as Pt(0). In some embodiments, at least a portion of the rhodium is present as Rh(0). In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 30 nm. In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 20 nm. In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 12 nm. In some embodiments, platinum is present in an amount up to about 1.4 wt %. In some embodiments, rhodium is present in an amount up to about 0.8 wt %.
  • the total amount of platinum and rhodium present is in the range of from about 0.2 wt % to about 2 wt %. In some embodiments, the total amount of platinum and rhodium present is in the range of from about 0.2 wt % to about 1.5 wt %.
  • the catalyst further comprises a metal selected from the group of palladium, molybdenum and tungsten. In some embodiments, the catalyst is a shell type catalyst the outer surfaces of which are impregnated with the metals so as to create a metal-impregnated outer shell having a thickness equal to or less than about 150 ⁇ m.
  • the present invention is also directed to catalysts comprising platinum and rhodium and a support at least the outer surfaces of which are selected from the group consisting of zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites and mixtures thereof, wherein the molar ratio of platinum to rhodium on the support is in the range of from about 3:1 to about 1:2, and the average pore diameter of the support is in the range of from about 5 nm to about 70 nm.
  • at least a portion of the platinum and rhodium are impregnated into the support so as to form a metal-impregnated outer shell surrounding a core of essentially un-impregnated support material.
  • the molar ratio of platinum to rhodium is in the range of about 3:1 to about 1:1.
  • the average pore diameter of the support is in the range of from about 5 nm to about 40 nm.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 200 m 2 /g. In some embodiments, the surface area of the support is in the range of between about 15 m 2 /g and about 125 m 2 /g. In some embodiments, the surface area of the support is in the range of between about 15 m 2 /g and about 60 m 2 /g. In some embodiments, at least a portion of the platinum is present as Pt(0).
  • the particle sizes of the metals are in the range of from about 2 nm to about 30 nm. In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 20 nm. In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 12 nm. In some embodiments, the total amount of platinum and rhodium present is equal to or less than about 2 wt %. In some embodiments, the total amount of platinum and rhodium present is in the range of from about 0.2 wt % to about 1.5 wt %.
  • the catalyst further comprises a metal selected from the group of palladium, molybdenum and tungsten.
  • the catalyst is a shell type catalyst the outer surfaces of which are impregnated with the metals so as to create a metal-impregnated outer shell having a thickness equal to or less than about 150 ⁇ m.
  • the present invention is also directed to processes for preparing adipic acid or derivatives thereof comprising reacting a substrate comprising material of the formula ROOC(CX) y COOR, where “y” is at least 2, “X” is, independently, selected from the group of hydroxyl, oxo, halo, acyloxy and hydrogen provided that at least one X is not hydrogen, and each “R” is, independently, selected from the group of salt-forming ions, hydrogen and hydrocarbyl or substituted hydrocarbyl or a mono- or di-lactone thereof, with hydrogen in the presence of a catalyst comprising platinum and rhodium and a support at least the outer surfaces of which support are selected from the group consisting of zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites and mixtures thereof, wherein the molar ratio of platinum to rhodium is in the range of from about 3:1 to about 1:2, to convert the substrate to adipic acid and/or derivative thereof.
  • the platinum and rhodium are impregnated into the support so as to form a metal-impregnated outer shell surrounding a core of essentially un-impregnated support material.
  • the molar ratio of platinum to rhodium is in the range of about 3:1 to about 1:1.
  • the average pore diameter of the support is in the range of from about 5 nm to about 70 nm. In some embodiments, the average pore diameter of the support is in the range of from about 5 nm to about 40 nm.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 200 m 2 /g.
  • the surface area of the support is in the range of between about 15 m 2 /g and about 125 m 2 /g. In some embodiments, the surface area of the support is in the range of between about 15 m 2 /g and about 60 m 2 /g. In some embodiments, at least a portion of the platinum is present as Pt(0). In some embodiments, at least a portion of the rhodium is present as Rh(0). In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 30 nm. In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 20 nm.
  • the particle sizes of the metals are in the range of from about 2 nm to about 12 nm.
  • the total amount of platinum and rhodium present is equal to or less than about 10 wt %. In other embodiments, the total amount of platinum and rhodium present is equal to or less than about 4 wt %. In some embodiments, the total amount of platinum and rhodium present is equal to or less than about 2 wt %. In some embodiments, the total amount of platinum and rhodium present is in the range of from about 0.2 wt % to about 1.5 wt %.
  • the present invention is also directed to catalysts comprising platinum and rhodium and a support at least the outer surfaces of which support are selected from the group consisting of zirconia and stabilized zirconia, wherein the molar ratio of platinum to rhodium in the range of from about 3:1 to about 1:1, the average pore diameter of the support is in the range of from about 5 nm to about 70 nm and the surface area of the support is in the range of between about 15 m 2 /g and about 125 m 2 /g.
  • at least a portion of the platinum and rhodium are impregnated into the support so as to form a metal-impregnated outer shell surrounding a core of essentially un-impregnated support material.
  • the average pore diameter of the support is in the range of from about 5 nm to about 40 nm. In some embodiments, the surface area of the support is in the range of between about 15 m 2 /g and about 60 m 2 /g. In some embodiments, at least a portion of the platinum is present as Pt(0). In some embodiments, at least a portion of the rhodium is present as Rh(0). In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 30 nm. In some embodiments, the particle sizes of the metals are in the range of from about 2 nm to about 20 nm.
  • the particle sizes of the metals are in the range of from about 2 nm to about 12 nm.
  • platinum is present in an amount up to about 1.4 wt %.
  • rhodium is present in an amount up to about 0.8 wt %.
  • the total amount of platinum and rhodium present is equal to or less than about 10 wt %.
  • the total amount of platinum and rhodium present is equal to or less than about 4 wt %.
  • the total amount of platinum and rhodium present is equal to or less than about 2 wt %.
  • the total amount of platinum and rhodium present is in the range of from about 0.2 wt % to about 1.5 wt %.
  • the catalyst further comprises a metal selected from the group of palladium, molybdenum and tungsten.
  • the catalyst is a shell type catalyst the outer surfaces of which are impregnated with the metals so as to create a metal-impregnated outer shell having a thickness equal to or less than about 150 ⁇ m.
  • the present invention is also directed to processes for producing an adipic acid product comprising reacting, in the presence of a catalyst comprising platinum and rhodium and a support at least the outer surfaces of which are selected from the group comprising zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites, and mixtures thereof, wherein the molar ratio of platinum to rhodium is in the range of from about 3:1 to about 1:2 and the total weight percent of platinum and rhodium is equal to or less than about 10 wt % (of the total catalyst weight), with a substrate of the general formula ROOC(CX) y COOR, where “y” is at least 2, “X” is, independently, selected from the group of hydroxyl, oxo, halo, acyloxy and hydrogen provided that at least one X is not hydrogen, and each “R” is, independently, selected from the group of salt-forming ions, hydrogen and hydrocarbyl or substituted hydrocarbyl or a mono
  • FIG. 1 is a TEM photograph of an example of a fresh catalyst prepared in accordance with the present invention comprising 0.6 wt % platinum and 0.2 wt % rhodium on a zirconia support wherein at least about 50% of the particle sizes of the metal particles are in the range of about 5-20 nm (magnification 88k ⁇ ).
  • FIG. 2 is a TEM photograph of an example of a fresh catalyst prepared in accordance with the present invention comprising 0.6 wt % platinum and 0.2 wt % rhodium on a zirconia support wherein at least about 50% of the particle sizes of the metal particles are in the range of about 5-10 nm (magnification 255k ⁇ ).
  • heterogeneous catalysts comprised of platinum and rhodium on a support at least the outer surfaces of which are zirconia, stabilized (doped) zirconia, zirconia-metal oxide composites or mixtures thereof.
  • the heterogeneous catalysts of the present invention are useful generally for selective hydrodeoxygenation. More particularly, the catalysts of the present invention are useful in the selective hydrodeoxygenation of compositions of the general formula ROOC(CX) y COOR, where “y” is at least 2, “X” is, independently, selected from the group of hydroxyl, oxo, halo, acyloxy and hydrogen provided that at least one X is not hydrogen, and each “R” is, independently, selected from the group of salt-forming ions, hydrogen and hydrocarbyl or substituted hydrocarbyl or a mono- or di-lactone thereof, to the corresponding dicarboxylic acids and derivative thereof of the general formula ROOC(CH) y COOR, wherein “y” is at least 2 and up to about 10, preferably between about 2 and 4, and each “R” is, independently, selected from the group of salt-forming ions, hydrogen and hydrocarbyl or substituted hydrocarbyl or a mono- or di-lactone thereof.
  • the catalysts of the present invention are heterogeneous, solid-phase catalysts.
  • the catalysts of the present invention comprise metals on at least the external surfaces (the “exposed surfaces”) of a support at least the outer surfaces of which are selected from the group of zirconia, stabilized (doped) zirconia, zirconia(or stabilized zirconia)-metal oxide composites and mixtures thereof.
  • the supports consist essentially of zirconia or stabilized (doped) zirconia.
  • a zirconia support means a support comprised of zirconia and no more than about 5 wt % of other materials, more typically less than about 2 wt %, not intentionally added to perform a specific function.
  • these “trace” materials are hafnium, silica and/or titania.
  • Zirconia exists in one or more crystalline phases: as essentially monoclinic, essentially tetragonal, monoclinic with a small fraction of tetragonal, or tetragonal with a small fraction of monoclinic.
  • Stabilized zirconia also referred as “doped” zirconia is zirconia in combination with one or more metal oxides intentionally added to stabilize one or more of the phases of which the zirconia may exist, and typically the addition(s) is(are) present to stabilize the tetragonal phase of zirconia.
  • Zirconia (or stabilized-zirconia)-metal oxide composites are shell and core composites wherein the zirconia (or stabilized zirconia) form the shell of the support and another metal oxide (or different zirconia or stabilized zirconia) forms the core of the support.
  • Useful core materials, in addition to zirconia or stabilized zirconia, include silicas or silicates, titanias and aluminas. Those of ordinary skill in the art are readily capable of producing useful composite catalyst supports.
  • the overall shape of the catalyst support is not critical.
  • the catalysts can be in the form of, for example, spheres, beads, cylinders, lobed shapes (for example, bi-, tri-, star-), holed (for example, rings, cored beads, spheres, cylinders, or lobe shapes), and the metal distribution on the surface of the support can be uniform or non-uniform.
  • the metal is distributed such that it forms a metal-impregnated outer shell having a thickness in the range of about 30 ⁇ m to about 150 ⁇ m, and more typically the thickness of the metal-impregnated outer shell is equal to or less than about 100 ⁇ m.
  • the catalysts of the present invention are particularly effective as hydrodeoxygenation catalysts in part because the surface area of the supports thereof are in the range of between about 15 m 2 /g and about 200 m 2 /g, preferably are in the range of between about 15 m 2 /g and about 125 m 2 /g, and more preferably equal to or less than about 60 m 2 /g. In various embodiments, the surface area of the supports are in the range of from about 15 m 2 /g to about 60 m 2 /g.
  • the average pore diameters of the supports of the present invention are in the range of at least about 5 nanometer (nm) to about 70 nanometer (nm), preferably in the range of from about 5 nm to about 40 nm, and exhibit a monomodal or multimodal pore size distribution.
  • the pore volume of the supports of the catalysts of the present invention are in the range of from about 0.1 ml/g to about 1.0 ml/g, and more typically are less than or equal to about 0.5 ml/g. Average pore diameters and pore volumes are determined in accordance with the procedures described in E. P. Barrett, L. G.
  • the catalysts of the present invention may be produced by deposition procedures known in the art including, but not limited to, incipient wetness, ion-exchange and deposition-precipitation and absorption from excess solution (volume higher than ion exchange or incipient wetness), physical vapor deposition, chemical vapor deposition, solution coating or wash coating.
  • a uniform dispersion can be effected by forming a heterogeneous slurry or suspension of the support in combination with solubilized metal complexes.
  • the supports may be initially dispersed in a liquid such as water; thereafter, in such embodiments, the solubilized metal complexes may be added to the slurry containing the support.
  • the heterogeneous mixture of solid and liquids can then be stirred, mixed and/or shaken or fluidized to enhance the uniformity of dispersion of the catalyst components which, in turn, enables the more uniform deposition of metals on the surface of the support upon removal of the liquids and undertaking additional treatments as may be needed to produce the catalyst (and more fully described hereinafter).
  • the opposite order of addition i.e. adding the support to the metal solution is also possible.
  • Platinum-containing compounds useful in the present invention include nitrogen containing compounds such as platinum (II)dinitrate, platinum (IV) nitrate, platinum oxynitrate, tetraamineplatinum (II) nitrate, tetraamineplatinum (II) hydrogenphosphate, tetraamineplatinum (II) hydrogencarbonate, tetraamineplatinum (II) hydroxide, ethanolaminehexahydroxyplatinate (IV) complex, alkali metal-hexahydroxyplatinate (IV) complexes, tetraalkylammoniumhexahydroxyplatinate (IV) complexes, platinum (II) acetylacetanoate, platinum (II) oxalate, diamine-platinum (II) nitrite, potassium-platinum (II) nitrite, potassium platinum (II) oxalate
  • platinum (II)dinitrate platinum (IV) chloride, and potassium or sodium tetrachloroplatinate (II).
  • the platinum precursor solutions can optionally be stabilized by mineral acids, ammonia, alkali metal solutions such as NaOH, alkali metal salts such as NaCl, ethanolamine or carboxylic acids such as glycolic acid or oxalic acid.
  • Rhodium-containing compounds useful in the present invention include ammonium hexachlororhodate (III), alkali metal-hexachlororhodate (III), hexaaminerhodium (III) hydroxide, hexaaminerhodium (III) chloride, rhodium sesquioxide hydrate, rhodium (III) acetylacetanoate, rhodium trinitrate, rhodium (III)trichloride, rhodium (III)acetate, and ethanolamine rhodium (II)acetate.
  • Some preferred compounds include rhodium (III)trichloride and rhodium (III)trinitrate.
  • the order of addition of the metal precursors in combination with the support material is not believed to be critical. Those of ordinary skill in the art will recognize that the metal-containing components can be combined with the support material sequentially (separate fix) or simultaneously (single fix). And, as described above, among other useful processes, the metal deposition can be accomplished by wet chemical impregnation techniques and/or by physical coating (for example, spraying of aerosols onto tumbling pellets).
  • the temperature(s) at which metal precursor deposition takes place can range from at or below ambient up to about 120° C. depending upon the deposition process selected, and those of ordinary skill in the art may readily select the appropriate deposition process and conditions to effectuate the deposition of the metal-containing compounds onto (and into) the support.
  • the metal-containing catalyst precursor may be dried. Drying may be conducted at ambient temperature or at an elevated temperature up to about 120° C. Preferably, drying is conducted at a temperature in the range of about 40° C. to about 90° C. and more preferably at a temperature at least about 60° C. The drying step may be conducted for a period of time ranging from about a few minutes to a few days. Typically, the drying time is in the range of about 6 hours to about 24 hours. Drying of the catalyst precursor can be conducted, for example, on a band dryer, in a direct fired rotary oven, or in an indirect fired rotary oven. When using physical coating for the metal deposition, drying may be done simultaneously with the coating step in the coating chamber. After deposition of the metal precursors an auxiliary chemical agent (e.g. precipitation agent) may be added, either before and/or after drying, to convert the precursors into more easily reducible or thermally decomposable forms.
  • auxiliary chemical agent e.g. precipitation agent
  • the support having the precursor compound deposited thereon and, possibly, therein is typically subjected to at least one thermal treatment, under oxidative (calcination), inert (nitrogen, argon) and/or reductive (gas phase or liquid phase reductants) conditions, as is necessary for the metals of the catalyst, in order to convert the platinum and rhodium deposited thereon to Pt(0) and Rh(0).
  • the catalysts may be calcined and then the metal may be further reduced to Pt(0) and Rh(0) in-situ (i.e., in the reactor).
  • platinum the platinum of the compound is reducible to Pt(0) upon thermal treatment regardless of whether the atmosphere is oxidizing, inert or reducing.
  • thermal treatment(s) may, for example, be conducted in air.
  • the substantial decomposition of the Pt precursor occurs during calcination and at least a portion of the platinum is converted to Pt(0).
  • the rhodium is preferably reduced to Rh(0) under reducing atmosphere conditions. Therefore, in various embodiments, the thermal treatment(s) is (are) conducted under a hydrogen gas containing atmosphere; alternatively, a liquid reducing agent may be employed to reduce the metals to platinum(0) and rhodium(0) on the support: for example, hydrazine, formaldehyde, formic acid, sodium formate or sodium hypophosphite may be employed to effect the requisite reduction.
  • the temperature(s) at which the calcination treatment(s) is (are) conducted generally range from about 150° C. to about 600° C. More typically, the temperature(s) of the thermal treatment(s) range from about 200° C. to about 550° C.
  • the thermal treatment is typically conducted for a period of time ranging from about 1 hour to about 16 hours. More typically, the treatment is conducted for a period of time ranging from about 2 hours to about 12 hours. For example, at a thermal treatment temperature of about 350° C., the time of the treatment at temperature is in the range of about 2 hours to about 6 hours.
  • a thermal treatment under such gas phase reductive conditions is generally conducted at a temperature range from about 100° C. to about 500° C.
  • the thermal treatment under liquid phase reductive conditions is conducted at a temperature range from about 20° C. to about 95° C.
  • a thermal treatment under reductive conditions can optionally be conducted in situ in a chemical reactor prior to the use of the catalyst given the reaction temperatures typically employed, for example, in the production of an adipic acid product from glucaric acid substrate.
  • a thermal treatment under reducing conditions can be conducted subsequent to a calcination treatment.
  • a washing step can be employed after a thermal treatment to remove non-decomposable counterion(s) of the metal precursor compounds, such as Na, K, Cl.
  • Typical wash solutions can include, for example, water, alcohols, polyols, carboxylic acids, or mixtures thereof.
  • the wash solution may optionally contain a chemical reagent that will complex the counterion(s).
  • the reduced metals deposited on the outer surfaces of the support are in the form of metallic particles: that is to say, the platinum on the fresh catalyst exists substantially as particles of substantially platinum (0) and the rhodium on the fresh catalyst exists substantially as particles of rhodium (0).
  • the metallic particles of the catalysts of the present invention are substantially of a size in the range of at least about 1 nanometer (nm) and less than or equal to about 30 nanometers (nm).
  • size we mean the largest, straight line dimension of the particle.
  • substantially we mean at least about 50%.
  • the particles are substantially of a size equal to or less than about 20 nm and, preferably, in the range of about 2 nm to about 20 nm (See, for example, the fresh catalyst photograph of FIG. 1 ). More preferably, the particles are at least substantially in the range of about 2 nm to about 12 nm as, for example, shown in the photograph of FIG. 2 .
  • the catalyst of the present invention is considered to be that catalyst which is intended to perform the reaction for which it was intended after any ramp up conditions which may be employed in catalytic reactions of this type.
  • the platinum to rhodium molar ratio of the catalyst of the present invention is in the range of from about 3:1 to about 1:2.
  • the platinum to rhodium molar ratio may vary, for example, from about 3:1 to about 1:1.
  • a third metal may be added to produce a Pt/Rh/M3 catalyst wherein the M3 metal is not platinum or rhodium.
  • a fourth metal may be added to produce a Pt/Rh/M3/M4 catalyst wherein the M4 metal is not platinum or rhodium and also not the same metal as the M3 metal.
  • the M3 metal and M4 metal may each be selected from group of palladium, ruthenium, iridium, gold, molybdenum, tungsten, niobium, tantalum, rhenium, and osmium. More preferably the M3 metal and M4 metal are selected from palladium, molybdenum and tungsten.
  • the total metal loading on the final catalyst is equal to or less than about 10 wt % of the total catalyst weight.
  • the total metal loading is in the range of from about 0.2 wt % to about 4 wt %.
  • metal loadings in the range of about 2 wt % or less are very effective in converting the substrates disclosed herein to the desired products.
  • metal loadings in the range of from about 0.2 wt % to about 1.5 wt % are particularly effective.
  • the catalysts comprise platinum in an amount up to about 1.4 wt % and rhodium in an amount up to about 0.8 wt %, and in various more preferred embodiments Pt is present in an amount in the range of from about 0.4 wt % to about 1.4 wt % and Rh is present in an amount in the range of from about 0.1 wt % to about 0.8 wt %.
  • the catalysts of the present invention are unexpectedly and particularly effective for the hydrodeoxygenation of compositions of the general formula ROOC(CX) y COOR, where “y” is at least 2, “X” is, independently, selected from the group of hydroxyl, oxo, halo, acyloxy and hydrogen provided that at least one X is not hydrogen, and each “R” is, independently, selected from the group of salt-forming ions, hydrogen and hydrocarbyl or substituted hydrocarbyl or a mono- or di-lactone thereof, to the corresponding dicarboxylic acids and derivative thereof having the general formula ROOC(CH) y COOR, where “y” is at least 2 and each “R” is, independently, selected from the group of salt-forming ions, hydrogen and hydrocarbyl or substituted hydrocarbyl or a mono- or di-lactone thereof. More particularly, glucaric acid and glucarolactones are, for example, effectively converted to adipic acid in high yield by reacting the same in the presence of
  • the reaction can be conducted in a batch, semi-batch, or continuous reactor design using fixed bed reactors, trickle bed reactors, slurry phase reactors, moving bed reactors, or any other design that allows for heterogeneous catalytic reactions.
  • reactors can be seen in Chemical Process Equipment—Selection and Design , Couper et al., Elsevier 1990, which is incorporated herein by reference. It should be understood that the substrate, hydrogen, any solvent, and the catalyst may be introduced into a suitable reactor separately or in various combinations.
  • hydrocarbyl refers to hydrocarbyl moieties, preferably containing 1 to about 50 carbon atoms, preferably 1 to about 30 carbon atoms, and even more preferably 1 to about 18 carbon atoms, including branched or unbranched, and saturated or unsaturated species.
  • Preferred hydrocarbyl can be selected from the group consisting of alkyl, alkylene, alkoxy, alkylamino, thioalkyl, haloalkyl, cycloalkyl, cycloalkylalkyl, heterocyclyl, N-heterocyclyl, heterocyclylalkyl, aryl, aralkyl heteroaryl, N-heteroaryl, heteroarylalkyl, and the like.
  • a hydrocarbyl may be optionally substituted hydrocarbyl.
  • various hydrocarbyls can be further selected from substituted alkyl, substituted cycloalkyl and the like.
  • Salt forming ions include, without limitation, for example ammonium ions and metal ions (e.g., alkali and alkaline earth metals).
  • R is a salt forming ion (i.e., a cation)
  • the carboxyl group may be considered to be an anion (i.e., carboxylate anion).
  • the hydrodeoxygenation substrate comprises a five or six carbon compound, wherein X is hydroxyl and R is independently a salt-forming ion, hydrogen, hydrocarbyl, or substituted hydrocarbyl.
  • X is hydroxyl
  • R is independently a salt-forming ion, hydrogen, hydrocarbyl, or substituted hydrocarbyl.
  • the hydrodeoxygenation substrate is a six carbon chain it has four chiral centers. As a result several stereoisomers are possible.
  • the hydrodeoxygenation substrate may comprise various ketones.
  • Ketones such as 2-keto-glucaric acid (2,3,4-trihydroxy-5-oxohexanedioic acid) and 3-keto-glucaric acid (2,3,5-trihydroxy-4-oxohexanedioic acid) are examples thereof.
  • the hydrodeoxygenation substrate may comprise various lactones which, in many embodiments are present in combination with glucaric acid.
  • various mono- and di-lactones are present in equilibrium with glucaric acid in aqueous solution, including for example, D-glucaro-1,4-lactone, D-glucaro-6,3-lactone, and D-glucaro-1,4:6,3-dilactone.
  • processes have been developed to quantitatively convert glucaric acid or a salt thereof in solution to one or more lactones and recover a substantially pure lactone stream.
  • the hydrodeoxygenation substrate comprises D-glucaro-1,4-lactone.
  • the hydrodeoxygenation substrate comprises D-glucaro-6,3-lactone. Still further, in these and other embodiments, the hydrodeoxygenation substrate comprises D-glucaro-1,4:6,3-dilactone. In these and other embodiments, the hydrodeoxygenation substrate comprises L-threo-4-deoxy-hex-4-enaro-6,3-lactone. Still even further, in these and other embodiments, the hydrodeoxygenation substrate comprises L-erythro-4-deoxy-hex-4-enaro-6,3-lactone.
  • an adipic acid product (formula II) may be prepared by reacting, in the presence of a catalyst of the present invention, a halogen source, a hydrodeoxygenation substrate of formula I and hydrogen, according to the following reaction:
  • the adipic acid product of formula II comprises adipic acid.
  • a hydrodeoxygenation substrate is converted to an adipic acid product by catalytic hydrodeoxygenation in which carbon-hydroxyl groups are converted to carbon-hydrogen groups.
  • the catalytic hydrodeoxygenation is hydroxyl-selective wherein the reaction is completed without substantial conversion of the one or more other non-hydroxyl functional group of the substrate.
  • the halogen source may be in a form selected from the group consisting of atomic, ionic, molecular, and mixtures thereof.
  • Halogen sources include hydrohalic acids (e.g., HCl, HBr, HI and mixtures thereof; preferably HBr and/or HI), halide salts, (substituted or unsubstituted) alkyl halides, or elemental halogens (e.g. chlorine, bromine, iodine or mixtures thereof; preferably bromine and/or iodine).
  • the halogen source is in molecular form and, more preferably, is bromine.
  • the halogen source is a hydrohalic acid, in particular hydrogen bromide.
  • the molar ratio of halogen to the hydrodeoxygenation substrate is about equal to or less than about 1.
  • the mole ratio of halogen to the hydrodeoxygenation substrate is typically from about 1:1 to about 0.1:1, more typically from about 0.7:1 to about 0.3:1, and still more typically about 0.5:1.
  • the reaction allows for recovery of the halogen source and catalytic quantities (where molar ratio of halogen to the hydrodeoxygenation substrate is less than about 1) of halogen can be used, recovered and recycled for continued use as a halogen source.
  • the temperature of the hydrodeoxygenation reaction mixture is at least about 20° C., typically at least about 80° C., and more typically at least about 100° C. In various embodiments, the temperature of the hydrodeoxygenation reaction is conducted in the range of from about 20° C. to about 250° C., from about 80° C. to about 200° C., more preferably from about 120° C. to about 180° C., and still more preferably between about 140° C. and 180° C.
  • the partial pressure of hydrogen is at least about 25 psia (172 kPa), more typically at least about 200 psia (1379 kPa) or at least about 400 psia (2758 kPa).
  • the partial pressure of hydrogen is from about 25 psia (172 kPa) to about 2500 psia (17237 kPa), from about 200 psia (1379 kPa) to about 2000 psia (13790 kPa), or from about 400 psia (2758 kPa) to about 1500 psia (10343 kPa).
  • the hydrodeoxygenation reaction is typically conducted in the presence of a solvent.
  • Solvents suitable for the selective hydrodeoxygenation reaction include water and carboxylic acids, amides, esters, lactones, sulfoxides, sulfones and mixtures thereof.
  • Preferred solvents include water, mixtures of water and weak carboxylic acid, and weak carboxylic acid.
  • a preferred weak carboxylic acid is acetic acid.
  • An adipic acid product may be recovered from the hydrodeoxygenation reaction mixture by one or more conventional methods known in the art including, for example, solvent extraction, crystallization or evaporative processes.
  • aqueous solution of a platinum precursor compound and rhodium precursor compound was added to supports of zirconia, titania, silica, carbon, zeolite and montmorillonite in the form of particles (Examples 1-4) and extrudate (Example 5) in multiple portions.
  • the metal precursor solution was either pipetted or sprayed onto the support for the impregnation. Each mixture was agitated to evenly impregnate the support. Each sample was dried in a 60° C. oven or at room temperature overnight under a dry air purge. Each sample was then reduced under forming gas (5% H 2 and 95% N 2 ) atmosphere typically at 350° C. for 6 hours with 2° C./min temperature ramp rate.
  • different metal precursor compounds can be used to prepare catalysts with various Rh and Pt metal loadings and molar ratios of Rh and Pt on different supports.
  • Rh and Pt precursor compounds were found to be incompatible (meaning formation of precipitate upon contact of solutions)
  • one metal precursor solution was added to the support to impregnate the support with one metal, followed by drying in a 60° C. oven or at room temperature overnight under a dry air purge, and subsequent addition of the other metal precursor solution was undertaken to impregnate the single metal containing support with the other metal.
  • the material was further dried in a 60° C. oven or at room temperature overnight under a dry air purge.
  • aqueous solution of platinum nitrate and rhodium nitrate (20 ml in total volume containing 0.41 g Rh and 1.17 g Pt) was added to a zirconia support (100 g, 90-180 ⁇ m particle size) in multiple portions using a pipette over a period of 10 min. During the addition of the solution, the mixture was agitated to evenly impregnate the support. The sample was dried in a 60° C. oven overnight under a dry air purge. The sample was then reduced under forming gas (5% H 2 and 95% N 2 ) atmosphere at 350° C. for 6 hours with 2° C./min temperature ramp rate. The final catalyst contained 0.41 wt % Rh and 1.17 wt % Pt.
  • the mixture was agitated to evenly impregnate the support.
  • the sample was dried in a 60° C. oven overnight under a dry air purge.
  • the sample was then reduced under forming gas (5% H 2 and 95% N 2 ) atmosphere at 350° C. for 6 hours with 2° C./min temperature ramp rate.
  • the final catalyst contained 0.24 wt % Rh and 0.54 wt % Pt.
  • Catalyst (20 mg) produced in accordance with the general description set forth hereinabove was weighed into a glass vial insert, followed by addition of a solution (100 1l in total volume) containing glucaric acid monolactone (0.8 M) and HBr (0.6 M) in acetic acid.
  • the glass vial insert was loaded into a pressure reactor and the reactor was closed.
  • the atmosphere in reactor was replaced with hydrogen and pressurized to 900 psig at room temperature.
  • Reactor was heated to 160° C. and maintained at 160° C. for 1.5 hours with orbital shaking. After 1.5 hours, the shaking was stopped and reactor was cooled to 40° C. Pressure in reactor was then slowly released.
  • the glass vial insert was removed from reactor and centrifuged.
  • Pt/Rh zirconia and Pt/Rh titania catalysts were prepared in accordance with the previous examples and tested for selective hydrodeoxygenation of glucaric acid monolactone in a continuous flow fixed bed reactor over a period of 100 hours.
  • the Pt/Rh zirconia catalyst was effective for the selective hydrodeoxygenation of glucaric acid monolactone without any appreciable loss of catalyst activity during the 100 hour test.
  • the Pt/Rh titania catalyst showed an appreciable loss of activity during the 100 hour test.
  • the final catalyst contained 0.20 wt % Rh and 0.60 wt % Pt located in a shell on the surface of the extrudate. This catalyst was effective for the selective hydrodeoxygenation of glucaric acid monolactone in a continuous flow fixed bed reactor over a period of 1000 hours without any appreciable loss of catalyst activity.

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